DE102013016701A1 - Process for the denitrification of bypass exhaust gases in a plant for the production of cement clinker - Google Patents
Process for the denitrification of bypass exhaust gases in a plant for the production of cement clinker Download PDFInfo
- Publication number
- DE102013016701A1 DE102013016701A1 DE102013016701.9A DE102013016701A DE102013016701A1 DE 102013016701 A1 DE102013016701 A1 DE 102013016701A1 DE 102013016701 A DE102013016701 A DE 102013016701A DE 102013016701 A1 DE102013016701 A1 DE 102013016701A1
- Authority
- DE
- Germany
- Prior art keywords
- bypass exhaust
- rotary kiln
- gas
- exhaust gas
- ceramic filter
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000007789 gas Substances 0.000 title claims abstract description 159
- 239000004568 cement Substances 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 31
- 238000004519 manufacturing process Methods 0.000 title claims description 16
- 230000008569 process Effects 0.000 title claims description 13
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 82
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 80
- 239000003054 catalyst Substances 0.000 claims abstract description 52
- 239000000919 ceramic Substances 0.000 claims abstract description 44
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 40
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims abstract description 36
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000004202 carbamide Substances 0.000 claims abstract description 35
- 239000000126 substance Substances 0.000 claims abstract description 32
- 238000001816 cooling Methods 0.000 claims abstract description 26
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- 230000002829 reductive effect Effects 0.000 claims abstract description 12
- 235000012054 meals Nutrition 0.000 claims abstract description 9
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims abstract description 7
- 150000001342 alkaline earth metals Chemical class 0.000 claims abstract description 6
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 48
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 44
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 claims description 36
- PQXKHYXIUOZZFA-UHFFFAOYSA-M lithium fluoride Chemical compound [Li+].[F-] PQXKHYXIUOZZFA-UHFFFAOYSA-M 0.000 claims description 36
- PUZPDOWCWNUUKD-UHFFFAOYSA-M sodium fluoride Chemical compound [F-].[Na+] PUZPDOWCWNUUKD-UHFFFAOYSA-M 0.000 claims description 36
- 239000011734 sodium Substances 0.000 claims description 25
- 239000011780 sodium chloride Substances 0.000 claims description 24
- 150000003467 sulfuric acid derivatives Chemical class 0.000 claims description 22
- 150000002013 dioxins Chemical class 0.000 claims description 21
- 150000002240 furans Chemical class 0.000 claims description 21
- GQPLMRYTRLFLPF-UHFFFAOYSA-N nitrous oxide Inorganic materials [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 claims description 21
- 239000001103 potassium chloride Substances 0.000 claims description 20
- 235000011164 potassium chloride Nutrition 0.000 claims description 20
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 claims description 16
- 238000002156 mixing Methods 0.000 claims description 16
- DZKDPOPGYFUOGI-UHFFFAOYSA-N tungsten(iv) oxide Chemical compound O=[W]=O DZKDPOPGYFUOGI-UHFFFAOYSA-N 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- 238000006722 reduction reaction Methods 0.000 claims description 11
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- 230000003647 oxidation Effects 0.000 claims description 8
- 238000007254 oxidation reaction Methods 0.000 claims description 8
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 7
- 150000004826 dibenzofurans Chemical class 0.000 claims description 7
- 238000005245 sintering Methods 0.000 claims description 7
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 6
- 229910052783 alkali metal Inorganic materials 0.000 claims description 5
- 150000001340 alkali metals Chemical class 0.000 claims description 5
- 229910052791 calcium Inorganic materials 0.000 claims description 5
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- 229910052700 potassium Inorganic materials 0.000 claims description 5
- 229910052708 sodium Inorganic materials 0.000 claims description 5
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 4
- 239000000470 constituent Substances 0.000 claims description 4
- INHCSSUBVCNVSK-UHFFFAOYSA-L lithium sulfate Inorganic materials [Li+].[Li+].[O-]S([O-])(=O)=O INHCSSUBVCNVSK-UHFFFAOYSA-L 0.000 claims description 4
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 claims description 4
- 229910052939 potassium sulfate Inorganic materials 0.000 claims description 4
- 235000011151 potassium sulphates Nutrition 0.000 claims description 4
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 4
- 235000011152 sodium sulphate Nutrition 0.000 claims description 4
- RBTVSNLYYIMMKS-UHFFFAOYSA-N tert-butyl 3-aminoazetidine-1-carboxylate;hydrochloride Chemical compound Cl.CC(C)(C)OC(=O)N1CC(N)C1 RBTVSNLYYIMMKS-UHFFFAOYSA-N 0.000 claims description 4
- 238000009434 installation Methods 0.000 claims 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 abstract description 2
- FVAUCKIRQBBSSJ-UHFFFAOYSA-M sodium iodide Chemical compound [Na+].[I-] FVAUCKIRQBBSSJ-UHFFFAOYSA-M 0.000 description 48
- 239000000460 chlorine Substances 0.000 description 19
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 18
- 229910002091 carbon monoxide Inorganic materials 0.000 description 17
- 229910004261 CaF 2 Inorganic materials 0.000 description 16
- HSZCZNFXUDYRKD-UHFFFAOYSA-M lithium iodide Inorganic materials [Li+].[I-] HSZCZNFXUDYRKD-UHFFFAOYSA-M 0.000 description 16
- 239000011698 potassium fluoride Substances 0.000 description 16
- NLKNQRATVPKPDG-UHFFFAOYSA-M potassium iodide Substances [K+].[I-] NLKNQRATVPKPDG-UHFFFAOYSA-M 0.000 description 16
- 235000013024 sodium fluoride Nutrition 0.000 description 16
- 239000011775 sodium fluoride Substances 0.000 description 16
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 11
- YLQBMQCUIZJEEH-UHFFFAOYSA-N Furan Chemical compound C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 10
- 229910052736 halogen Inorganic materials 0.000 description 10
- 150000002367 halogens Chemical class 0.000 description 10
- 238000002485 combustion reaction Methods 0.000 description 9
- 239000000428 dust Substances 0.000 description 9
- 239000000567 combustion gas Substances 0.000 description 7
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 description 6
- 239000001569 carbon dioxide Substances 0.000 description 6
- 229910052801 chlorine Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 5
- 239000004744 fabric Substances 0.000 description 5
- 238000002347 injection Methods 0.000 description 5
- 239000007924 injection Substances 0.000 description 5
- 239000010457 zeolite Substances 0.000 description 5
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 4
- 229910021536 Zeolite Inorganic materials 0.000 description 4
- 229910001615 alkaline earth metal halide Inorganic materials 0.000 description 4
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000011575 calcium Substances 0.000 description 3
- 239000000292 calcium oxide Substances 0.000 description 3
- 235000012255 calcium oxide Nutrition 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003863 metallic catalyst Substances 0.000 description 3
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- 238000010791 quenching Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 2
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- 239000006229 carbon black Substances 0.000 description 2
- 150000001722 carbon compounds Chemical class 0.000 description 2
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- 230000008021 deposition Effects 0.000 description 2
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- 230000000171 quenching effect Effects 0.000 description 2
- BUHVIAUBTBOHAG-FOYDDCNASA-N (2r,3r,4s,5r)-2-[6-[[2-(3,5-dimethoxyphenyl)-2-(2-methylphenyl)ethyl]amino]purin-9-yl]-5-(hydroxymethyl)oxolane-3,4-diol Chemical compound COC1=CC(OC)=CC(C(CNC=2C=3N=CN(C=3N=CN=2)[C@H]2[C@@H]([C@H](O)[C@@H](CO)O2)O)C=2C(=CC=CC=2)C)=C1 BUHVIAUBTBOHAG-FOYDDCNASA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 238000001321 HNCO Methods 0.000 description 1
- OWIKHYCFFJSOEH-UHFFFAOYSA-N Isocyanic acid Chemical compound N=C=O OWIKHYCFFJSOEH-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910010413 TiO 2 Inorganic materials 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
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- 230000015556 catabolic process Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
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- 229910052811 halogen oxide Inorganic materials 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
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- 230000007306 turnover Effects 0.000 description 1
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Classifications
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- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/364—Avoiding environmental pollution during cement-manufacturing
- C04B7/365—Avoiding environmental pollution during cement-manufacturing by extracting part of the material from the process flow and returning it into the process after a separate treatment, e.g. in a separate retention unit under specific conditions
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Abstract
Die Erfindung betrifft ein Verfahren zur Entstickung von Bypassabgasen (105, 205, 305) in einer Anlage zur Herstellung von Zementklinker, wobei die Anlage in Gasflussrichtung einen Drehrohrofen (102, 202, 302) aufweist, und wobei der Drehrohrofen (102, 202, 302) über eine Drehrohrofeneinlaufkammer (104, 204, 304) mit einem Calcinator (107, 207, 307) zur Entsäuerung von Rohmehl oder mit einem Drehrohrofensteigeschacht verbunden ist, und wobei das Bypassabgas im Bereich der Drehrohrofeneinlaufkammer (104, 204, 304) abgezogen wird. Erfindungsgemäß ist vorgesehen, das Abkühlen des Bypassabgases (105, 205, 305) auf eine Temperatur zwischen 260°C und 400°C in einer Vorrichtung zum Kühlen, Eindüsen einer ammoniak-, harnstoff- und/oder ammoniumhaltigen Substanz in das gekühlte Bypassabgas (112, 21, 312), Einleiten des mit ammoniak-, harnstoff- und/oder ammoniumhaltiger Substanz vermischten und gekühlten Bypassabgases (112, 21, 312) in eine keramische Filteranordnung (114, 214, 314), in welcher beim vorherigen Abkühlen des Bypassabgases (112, 21, 312) ausgefallenes Halogenid und Sulfat der Alkali- und Erdalkalimetalle ausgefiltert werden, noch nicht durch die ammoniak-, harnstoff- und/oder ammoniumhaltigen (NH4 +) Substanz umgesetzten Stickoxide an einem in der keramischen Filteranordnung (114) vorhandenen und/oder der keramischen Filteranordnung (214, 314) unmittelbar folgenden vorhandenen Katalysator (116, 216, 316) chemisch selektiv reduziert werden.The invention relates to a method for denitrification of bypass exhaust gases (105, 205, 305) in a plant for producing cement clinker, wherein the plant in the gas flow direction has a rotary kiln (102, 202, 302), and wherein the rotary kiln (102, 202, 302 ) is connected via a rotary kiln inlet chamber (104, 204, 304) to a calciner (107, 207, 307) for deacidifying raw meal or to a rotary kiln riser, and wherein the bypass exhaust gas is withdrawn in the region of the rotary kiln inlet chamber (104, 204, 304). According to the invention, the cooling of the bypass exhaust gas (105, 205, 305) to a temperature between 260 ° C. and 400 ° C. in a device for cooling, injecting an ammonia, urea and / or ammonium-containing substance into the cooled bypass exhaust gas (112 , 21, 312), introducing the bypass exhaust gas (112, 21, 312) which has been mixed and cooled with ammonia, urea and / or ammonium-containing substance into a ceramic filter arrangement (114, 214, 314), in which the bypass exhaust gas is cooled beforehand ( 112, 21, 312) precipitated halide and sulfate of the alkali and alkaline earth metals are filtered out, not yet by the ammonia, urea and / or ammonium-containing (NH4 +) substance reacted nitrogen oxides present in a ceramic filter assembly (114) and / or the ceramic filter assembly (214, 314) immediately following existing catalyst (116, 216, 316) are chemically selectively reduced.
Description
Die Erfindung betrifft ein Verfahren zur Entstickung von Bypassabgasen in einer Anlage zur Herstellung von Zementklinker, wobei die Anlage in Gasflussrichtung einen Drehrohrofen zur Sinterung des Zementklinkers aufweist, und wobei der Drehrohrofen über eine Drehrohrofeneinlaufkammer mit einem Calcinator zur Entsäuerung von Rohmehl oder mit einem Drehrohrofensteigeschacht verbunden ist, und wobei das Bypassabgas im Bereich der Drehrohrofeneinlaufkammer abgezogen wird.The invention relates to a method for denitrification of bypass exhaust gases in a plant for the production of cement clinker, wherein the plant in the gas flow direction comprises a rotary kiln for sintering the cement clinker, and wherein the rotary kiln is connected via a Drehrohrofeneinlaufkammer with a calciner for deacidifying raw meal or with a rotary kiln riser shaft , And wherein the bypass exhaust gas is withdrawn in the region of the rotary kiln inlet chamber.
Zur Herstellung von Zement wird silikat- (SiO4 4–) und carbonathaltiges (CO3 2–) Gestein vermahlen, formal von Kohlendioxid (CO2) durch Entsäuerung des Carbonats (CO3 2–) zum Oxid (-O) (in Form von gebranntem Kalk, CaO) in der Wärme befreit, und in einem anschließenden Schritt wird das Gemisch aus silikathaltigem (SiO4 4–) und carbonathaltigem (CO3 2–) Rohmehl zu Zementklinker (ein Mischkristall aus Calciumsilikaten verschiedener Stöchiometrie) in einem Drehrohrofen in der Wärme gesintert. Die Sinterung findet bei vergleichsweise hohen Temperaturen statt, die bis zu 1.450°C reichen. Um diese hohen Temperaturen in einem Drehrohrofen zu erzeugen, sind im Drehrohrofen Brennerflammen notwendig, die eine Temperatur von 1.800°C bis zu 2.000°C aufweisen. Bei diesen hohen Temperaturen entstehen Stickoxide (NOx) durch Verbrennung des in der atmosphärischen Luft enthaltenen Stickstoffs (N2). Neben der Verbrennung des Luftstickstoffs (N2) ist eine weitere Stickoxidquelle ggf. im Brennstoff vorhanden, der zur Erzeugung der Wärme im Drehrohrofen verwendet wird. Dieser liegt in der Regel als chemisch gebundener Stickstoff (R-N) vor, beispielsweise als Amine (R-NH2) in organischen Sekundärbrennstoffen. Stickoxide (NOx) disproportionieren in der Feuchtigkeit der atmosphärischen Luft zu verschiedenen Sauerstoffsäuren des Stickstoffs mit unterschiedlicher Stöchiometrie. Diese Sauerstoffsäuren des Stickstoffs sind die Ursache des unerwünschten sauren Regens, der bei entsprechender Menge den pH-Wert von Wald- und Ackerböden unerwünscht verringert und dadurch die Resistenz von Bäumen und Pflanzen gegenüber Krankheiten sehr stark vermindert. Es sind daher gesetzliche Auflagen zur Vermeidung von Stickoxidemissionen zu beachten, die stets strenger werden. Das bedeutet, die absoluten Emissionen sind stets weiter zu verringern.For the production of cement silicate (SiO 4 4- ) and carbonate (CO 3 2- ) rock is ground, formally by carbon dioxide (CO 2 ) by deacidification of the carbonate (CO 3 2- ) to the oxide (-O) (in the form calcined lime, CaO), and in a subsequent step, the mixture of silicate-containing (SiO 4 4- ) and carbonate (CO 3 2- ) raw meal becomes cement clinker (a mixed crystal of calcium silicates of various stoichiometry) in a rotary kiln the heat sintered. The sintering takes place at comparatively high temperatures, which reach up to 1,450 ° C. To produce these high temperatures in a rotary kiln burner torches are required in the rotary kiln, which have a temperature of 1,800 ° C up to 2,000 ° C. At these high temperatures, nitrogen oxides (NO x ) are produced by combustion of the nitrogen contained in the atmospheric air (N 2 ). In addition to the combustion of the atmospheric nitrogen (N 2 ), another nitrogen oxide source may be present in the fuel, which is used to generate the heat in the rotary kiln. This is usually present as chemically bound nitrogen (RN), for example as amines (R-NH 2 ) in organic secondary fuels. Nitrogen oxides (NO x ) disproportionate in the humidity of the atmospheric air to various oxygen acids of the nitrogen with different stoichiometry. These oxygen acids of nitrogen are the cause of the unwanted acid rain, which undesirably reduces the pH value of forest and agricultural soils and thus greatly reduces the resistance of trees and plants to diseases. It is therefore necessary to comply with legal requirements to avoid nitrogen oxide emissions, which are becoming ever stricter. This means that the absolute emissions must always be further reduced.
Es ist nicht nur der Ausstoß von Stickoxiden (NOx) ein unerwünschtes Problem bei der Herstellung von Zement. Außer der Stickoxidemission ist es auch notwendig, den Zementklinker frei von Halogeniden (F–, Cl–, I–), und Sulfaten (SO4 2–) zu halten. Die Halogenide (F–, Cl–, I–), insbesondere die Chloride (Cl–) und die Sulfate (SO4 2–) der Alkali- (Li, Na, K) und Erdalkalimetalle (Mg, Ca) haben eine stark negative Auswirkung auf die Eigenschaften des aus dem Zementklinker herzustellenden Zements. Auch stören die Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogenide (MgF2, MgCl2, MgCl2, CaF2, CaCl2, CaI2) und -sulfate (Li2SO4 , Na2SO4, K2SO4, MgSO4, CaSO4) bei der Kondensation in der Drehofeneinlaufkammer. Die Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogenide (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfate (Li2SO4 , Na2SO4, K2SO4, MgSO4, CaSO4) gehen bei entsprechend hoher Temperatur im Drehrohrofen in den Gasraum über, was zunächst einen gewünschten Reinigungseffekt auf den Zementklinker bei dessen Sinterung ausübt. Beim Übergang der heißen Brennergase in einen Calcinator oder in einen Drehrohrofensteigeschacht, wo die Temperatur des Drehrohrofenabgases aufgrund der Abgabe der in dem Drehrohrofenabgas enthaltenen Wärme an die endotherme Entsäuerungsreaktion des Carbonats (CO3 2–) zu gebranntem Kalk (CaO) abrupt abnimmt, kondensieren die Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogenide (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfate (Li2SO4, Na2SO4, K2SO4, MgSO4, CaSO4) und erzeugen bei weiterer Abkühlung durch Erstarrung Anbackungen an den Wandungen der Drehrohrofeneinlaufkammer, die schließlich die Anlage zusetzen können.Not only is the emission of nitrogen oxides (NO x ) an undesirable problem in the production of cement. Apart from nitrogen oxide emissions, it is also necessary to keep the cement clinker free of halides (F - , Cl - , I - ), and sulfates (SO 4 2- ). The halides (F - , Cl - , I - ), especially the chlorides (Cl - ) and the sulfates (SO 4 2- ) of the alkali (Li, Na, K) and alkaline earth metals (Mg, Ca) have a strong negative Effect on the properties of the cement to be produced from the cement clinker. Also disturb the alkali (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth halides (MgF 2 , MgCl 2 , MgCl 2 , CaF 2 , CaCl 2 , CaI 2 ) and sulfates (Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ) during the condensation in the rotary kiln inlet chamber. The alkali metal (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth metal halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ) and sulfates (Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ) pass at a correspondingly high temperature in the rotary kiln into the gas space, which initially exerts a desired cleaning effect on the cement clinker during its sintering. When the hot burner gas passes into a calciner or into a rotary kiln riser pit where the temperature of the rotary kiln exhaust gas decreases abruptly due to the discharge of the heat contained in the rotary kiln exhaust gas to the endothermic acidification reaction of the carbonate (CO 3 2- ) to burnt lime (CaO) Alkali (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ) and sulfates (Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ) and produce on further cooling by solidification caking on the walls of the rotary kiln inlet chamber, which can eventually enforce the system.
Um die Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogenide (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfate (Li2SO4, Na2SO4, K2SO4, MgSO4, CaSO4) aus dem Prozess zu entfernen, ist es nach der Lehre in der
Eine dritte Emission, die zu vermeiden ist, ist der gemeinsam mit der staubbefreiten Abluft der Bypassabgase passierende Ausstoß von unerwünschten chlorierten und polychlorierten Dibenzodioxinen, umgangssprachlich und vereinfacht oft als „Dioxine” bezeichnet, und der Ausstoß von unerwünschten chlorierten polychlorierten Dibenzofuranen, umgangssprachlich und vereinfacht oft als „Furane” bezeichnet.A third issue to avoid is the emission of undesirable chlorinated and polychlorinated dibenzodioxins, commonly referred to as "dioxins", together with the dust-removed exhaust air of the by-pass exhaust gases, and the ejection of undesirable chlorinated polychlorinated dibenzofurans, colloquially and often simplified referred to as "furans".
Dioxine und Furane bilden sich bei Verbrennungsprozessen spontan in Präsenz von Kohlenstoff (C), Halogenen (F2, Cl2, I2) und Sauerstoff (O2). Die Verbrennungsführung kann bei der Verwendung von schwer im Abbrandverhalten kontrollierbarer Sekundärbrennstoffe unzureichend stattfinden, wobei beispielsweise halogenhaltige Lösemittel bei unvollständiger Verbrennung auch Halogenoxide bilden, die in der Wärme des Drehrohrofens zerfallen und dadurch freies Halogen (Cl2) entstehen lassen. Aufgrund der recht hohen Temperaturen in einem Drehrohrofen ist aber nicht mit einer Dioxin- und Furanbildung im Drehrohrofen zu rechnen, so dass Drehrohrofenabgase und Bypassabgase frei sein sollten von Dioxinen und Furanen. Aber die zur Entstaubung von Bypassabgasen häufig eingesetzten Elektro-Staubfilter, die aufgrund der hohen statischen Ladung gelegentlich zu Überschlägen neigen, können bei der Präsenz von Halogenen (F2, Cl2, I2) neben Kohlenstoffverbindungen und Sauerstoff (O2) Dioxine und Furane erzeugen, wobei Halogene (F2, Cl2, I2), speziell Chlor (Cl2), wie oben erwähnt, aus der Verbrennung von Sekundärbrennstoffen stammen oder mit dem Rohmehl eigentragen werden. Die Dioxine und die Furane bilden sich bei mäßiger Hitze im Staubabscheider aus in dem Bypassabgas enthaltenem Kohlenmonoxid (CO), Kohlendioxid (CO2), ggf. aus Ruß (Cx) und aus Chlor (Cl2) in Verbindung mit Luftsauerstoff (O2). Dioxine und Furane bilden sich – trotz ihrer vergleichsweise komplexen Struktur – unter diesen Bedingungen spontan. Dioxins and furans spontaneously form in combustion processes in the presence of carbon (C), halogens (F 2 , Cl 2 , I 2 ) and oxygen (O 2 ). The combustion management can take place inadequately with the use of secondary fuels which are difficult to control in the combustion behavior, for example halogen-containing solvents which form incomplete combustion and also form halogen oxides which decompose in the heat of the rotary kiln and thereby give rise to free halogen (Cl 2 ). Due to the rather high temperatures in a rotary kiln, however, no dioxin and furan formation in the rotary kiln is to be expected, so that rotary kiln exhaust gases and bypass exhaust gases should be free of dioxins and furans. However, electrostatic dust filters often used to dedust bypass exhaust gases, which are prone to flashovers due to their high static charge, can contain dioxins and furans in addition to carbon compounds and oxygen (O 2 ) in the presence of halogens (F 2 , Cl 2 , I 2 ) where halogens (F 2 , Cl 2 , I 2 ), especially chlorine (Cl 2 ), as mentioned above, are derived from the combustion of secondary fuels or will be carried with the raw meal. The dioxins and the furans are formed at moderate heat in the dust from carbon monoxide (CO) contained in the bypass exhaust, carbon dioxide (CO 2 ), possibly carbon black (C x ) and chlorine (Cl 2 ) in conjunction with atmospheric oxygen (O 2 ). Despite their comparatively complex structure, dioxins and furans spontaneously form under these conditions.
Im Prozess entstehen also Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogenide (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfate (Li2SO4, Na2SO4, K2SO4, MgSO4, CaSO4), Stickoxide (NOx) und auch Dioxine und Furane. Diese Stoffe müssen aus dem Prozess entfernt werden und sollen nicht in die freie Atmosphäre gelangen.Alkali (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ) and sulfates ( Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ), nitrogen oxides (NO x ) and also dioxins and furans. These substances must be removed from the process and should not be released into the free atmosphere.
In der
Eine Dioxin- und Furanvermeidung durch im Kreislauf geführte Bypassabgase führt also zu neuen Problemen, die bewältigt werden müssen.A dioxin and furan avoidance by circulating bypass exhaust gases thus leads to new problems that need to be overcome.
Darüberhinaus existieren im Stand der Technik Verfahren, die Bypassabgase mit den Abgasen eines Wärmetauschers, der in Gasströmungsrichtung noch hinter dem Calcinator oder hinter dem Drehrohrofensteigeschacht liegt, zu vermischen. Auf diese Weise werden die vom Gesetzgeber zulässigen Konzentrationen an unerwünschten Emissionen, hier insbesondere die Konzentration von Stickoxiden (NOx) im Gesamtabgas der Anlage zur Herstellung von Zement durch Verdünnen verringert. Dieses Verfahren führt aber nicht zur Verringerung der tatsächlichen Emissionen in absoluten Mengen. Des Weiteren werden vom Gesetzgeber in Zukunft auch Emissionsvorschriften erwartet, die dem Anlagenbetreiber ein Verdünnungsverbot für unerwünschte Emissionen auferlegen.Moreover, there exist in the prior art method, the bypass exhaust gases with the exhaust gases of a heat exchanger, which is located in the gas flow direction behind the calciner or behind the rotary kiln riser shaft to mix. In this way, the legislator's allowable concentrations of undesirable emissions, in particular the concentration of nitrogen oxides (NO x ) in the total exhaust gas of the plant for the production of cement by dilution are reduced. However, this method does not lead to a reduction in actual emissions in absolute quantities. Furthermore, emission regulations are expected by the legislature in the future, which impose a dilution ban on undesirable emissions for the plant operator.
Eine Stickoxid-, Dioxin- und Furanvermeidung durch Vermischung der Bypassabgase mit anderen aus dem Prozess entweichenden Gasen ist somit auch kein gangbarer Weg.A nitrogen oxide, dioxin and Furanvermeidung by mixing the bypass exhaust gases with other gases escaping from the process is therefore not a viable option.
Ein Verfahren, das zur Entstickung der Gesamtabgase einer Anlage zur Herstellung von Zement bekannt ist, ist das sogenannte SNCR-Verfahren (selective non catalytic reduction). Bei diesem Verfahren wird Ammoniak (NH3) in Gasform, Harnstoff (CH4N2O) und/oder eine Ammoniumlösung (NH4 +) an geeigneten Stellen der Anlage zur Herstellung von Zement eingedüst. Der Ammoniak (NH3), der Harnstoff (CH4N2O) und/oder die Ammoniumlösung (NH4 +) soll unter entsprechender Verweildauer und im richtigen Temperaturfenster mit den Stickoxiden (NOx) in der Abluft des Drehrohrofens, das durch die gesamte Anlage fließt, reagieren, und dabei aus Ammoniak (NH3) und Stickoxiden (NOx) Stickstoff (N2) und Wasser (H2O) bilden. Als geeigneter Ort wurde im Stand der Technik dafür der Kopf eines Calcinators gewählt. Die hohen Strömungsgeschwindigkeiten und der große Durchmesser der Anlage (4 m bis 8 m) und auch die hohe Belastung der in der Anlage geführten Gase mit Rohmehl machen aber eine quantitative Umsetzung der Stickoxide (NOx) nur schwer beherrschbar. Die Verweilzeit und die Strömung, sowie die störende Staubatmosphäre machen eine Entstickung mit Ammoniak (NH3) in einer Anlage zur Herstellung von Zement nur schwer beherrschbar. Entweder wird ein Stickoxidschlupf (NOx), ein Ammoniakschlupf (NH3) und/oder ein Lachgasschlupf (N2O), gegebenenfalls sogar ein Isocyansäureschlupf (HNCO) erreicht und nur mit einem unzureichendem Zeitanteil werden die gesamten in der Anlage geführten Gase durch Ammoniak (NH3), Harnstoff (CH4N2O), oder Ammoniumverbindungen (NH4 + X–) entstickt. In der übrigen Zeit findet der erwähnte Schlupf statt. Dazu kommt, dass die Verbrennung in der Anlage zur Herstellung von Zement bewusst gestuft durchgeführt wird, wodurch ein Wechsel von chemisch oxidativer und reduktiver Umgebung erfolgt und dadurch wird eine Reaktion von Kohlenmonoxid (CO) mit den Stickoxiden (NOx) erzwungen, in welchem Stickstoff (N2) und Kohlendioxid (CO2) entsteht. Die Stickoxide (NOx) werden mit Kohlenmonoxid (CO) chemisch reduziert. Die Entstickung mit dem SNCR-Verfahren zur Gesamtentstickung der gesamten Abgase der Ablage ist somit bisher auch nicht in zufriedenstellendem Maße gelungen.A process known for denitrification of the total emissions of a plant for the production of cement, the so-called SNCR (selective non-catalytic reduction). In this process, ammonia (NH 3 ) in gaseous form, urea (CH 4 N 2 O) and / or an ammonium solution (NH 4 + ) are injected at suitable points in the plant for the production of cement. The ammonia (NH 3 ), the urea (CH 4 N 2 O) and / or the ammonium solution (NH 4 + ) is under appropriate residence time and in the correct temperature window with the nitrogen oxides (NO x ) in the exhaust air of the rotary kiln, by the Whole plant flows, react, and thereby form ammonia (NH 3 ) and nitrogen oxides (NO x ) nitrogen (N 2 ) and water (H 2 O). As a suitable place for the head of a calciner was chosen in the prior art. However, the high flow velocities and the large diameter of the plant (4 m to 8 m) and also the high load of raw gas in the plant make a quantitative conversion of nitrogen oxides (NO x ) difficult to control. The residence time and the flow, as well as the disturbing dust atmosphere make denitrification with ammonia (NH 3 ) in a plant for the production of cement difficult to control. Either a nitrogen oxide slip (NO x ), an ammonia slip (NH 3 ) and / or or nitrous oxide (N 2 O), possibly even an isocyanic acid (HNCO) hatch, and only with an insufficient amount of time are all the gases in the plant ammonia (NH 3 ), urea (CH 4 N 2 O), or ammonium compounds ( NH 4 + X - ). In the remaining time, the mentioned slip takes place. In addition, the combustion in the plant for the production of cement is carried out deliberately stepped, whereby a change of chemical oxidative and reductive environment takes place and thereby a reaction of carbon monoxide (CO) is enforced with the nitrogen oxides (NO x ), in which nitrogen (N 2 ) and carbon dioxide (CO 2 ) is formed. The nitrogen oxides (NO x ) are chemically reduced with carbon monoxide (CO). The denitrification with the SNCR method for total denitrification of the entire exhaust gases of the filing has thus far not succeeded satisfactorily.
Eine Entstickung der Gesamtabgase mit dem SNCR-Verfahren ist somit auch kein gangbarer Weg.Denitrification of the total exhaust gases with the SNCR process is therefore not a viable option.
Auch ist die Konzentration auf die Entstickung der stark mit Stickoxiden (NOx) belasteten Drehrohrofenabgase über das SNCR-Verfahren kein gangbarer Weg, weil das dazu notwendige Temperaturfenster von ca. 950°C bis 1.000°C im Bypassabgas nicht erreicht wird. Bei geringeren Temperaturen findet zwar ein nicht unerheblicher Umsatz statt, aber eine quantitative chemische Reduktion der Stickoxide findet unterhalb des Temperaturfensters von ca. 950°C bis 1.000°C nicht statt. Des Weiteren muss das Bypassabgas zum Auskondensieren von Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogeniden (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfaten (Li2SO4 , Na2SO4, K2SO4, MgSO4, CaSO4) stark gekühlt werden. Dazu wäre es denkbar, das Bypassabgas erst mit dem SNCR-Verfahren zu entsticken und dann die Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogenide (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfate (Li2SO4 , Na2SO4, K2SO4, MgSO4, CaSO4) auszukondensieren. Aber dies würde eine Aufheizung der Bypassabgase erfordern und auch, den Prozess der Entstickung in Gegenwart der im Gasraum befindlichen Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogeniden (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfaten (Li2SO4 , Na2SO4, K2SO4, MgSO4, CaSO4) durchzuführen, was dann wiederum zu einem Schlupf von Ammoniak (NH3), Stickoxiden (NOx) und/oder Lachgas (N2O), gegebenenfalls Isocyansäureschlupf (HNCO) führt.Also, the concentration on the denitrification of heavily loaded with nitrogen oxides (NO x ) rotary kiln exhaust gases via the SNCR process is not a viable option, because the required temperature window of about 950 ° C to 1000 ° C in the bypass exhaust gas is not achieved. At lower temperatures, although a considerable turnover takes place, but a quantitative chemical reduction of nitrogen oxides does not take place below the temperature window of about 950 ° C to 1000 ° C. Furthermore, the bypass exhaust gas has to condense out of alkali (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ). and sulfates (Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ) are strongly cooled. For this purpose, it would be conceivable to de-embroider the bypass exhaust gas first with the SNCR method and then the alkali metal (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth metal halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ) and sulfates (Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ) to condense. But this would require heating of the bypass exhaust gases and also the process of denitrification in the presence of the alkali gas (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ) and sulfates (Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ), which in turn leads to slippage of ammonia (NH 3 ), nitrogen oxides (NO x ) and / or nitrous oxide (N 2 O), optionally Isocyanansäureschlupf (HNCO) leads.
Wenngleich die Entfernung von Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogeniden (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfaten (Li2SO4, Na2SO4, K2SO4, MgSO4, CaSO4) aus Bypassabgasen heute ein geringeres Problem darstellt, so sind die damit einhergehend notwendige Entstickung und die Vermeidung der Emission von Dioxinen und Furanen weiterhin verbesserungswürdig.Although the removal of alkali (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ) and sulfates ( Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ) from bypass exhaust gases represents a minor problem today, so the necessary denitrification and the avoidance of the emission of dioxins and furans are in need of improvement.
Aufgabe der Erfindung ist es daher, ein Verfahren zur Entstickung von Bypassabgasen zur Verfügung zu stellen.The object of the invention is therefore to provide a method for denitrification of bypass exhaust gases.
Die erfindungsgemäße Aufgabe wird gelöst durch Abkühlen des Bypassabgases auf eine Temperatur zwischen 260°C und 400°C, bevorzugt zwischen 280°C bis 380°C in einer Vorrichtung zum Kühlen, vorzugsweise durch Vermischen des Bypassabgases mit Luft und/oder Wasser in einer Bypassmischkammer, Eindüsen einer ammoniak- (NH3), harnstoff- (CH4N2O), und/oder ammoniumhaltigen (NH4 +) Substanz in das gekühlte Bypassabgas, wobei der Ammoniak (NH3), der Harnstoff (CH4N2O) und/oder das Ammonium (NH4 +) die in dem abgekühlten Bypassabgas (
Nach der Erfindung ist also vorgesehen, dass das aus der Drehrohrofeneinlaufkammer abgezogene Bypassabgas, das selbst einen hohen Anteil von Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogeniden (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfaten (Li2SO4 , Na2SO4, K2SO4, MgSO4, CaSO4) im Gasraum aufweist, zunächst in einer Vorrichtung zum Kühlen abzuschrecken. Die Abkühlung der Bypassabgase findet dabei vorzugsweise in einer Mischkammer statt, in welcher sich die heißen Bypassabgase innig mit frischer atmosphärischer Luft oder mit Wasser vermischen. Dabei werden die heißen Bypassabgase auf eine Temperatur von 260°C bis 400°C, bevorzugt von 280°C bis 380°C abgekühlt. Bei dieser starken Abkühlung resublimieren die Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogenide (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfate (Li2SO4 , Na2SO4, K2SO4, MgSO4, CaSO4) und liegen als Staub neben Rohmehl im Bypassabgas vor. Die abgekühlte, stark Staubhaltige Luft wird sodann mit einer ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltigen (NH4 +) Substanz vermischt, in dem beispielsweise gasförmiges Ammoniakgas (NH3), eine wäßrige Harnstofflösung (CH4N2O) oder eine wässrige Ammoniumlösung (NH4 +) dem zwischen zwischen 260°C und 400°C, bevorzugt 280°C und 380°C betragenden, abgekühlten Bypassgas zugeführt wird. Bei dieser für die SNCR-Reaktion deutlich zu geringen Temperatur findet nur eine teilweise bis geringe Umsetzung von Stickoxiden (NOx) statt. Durch die Eindüsung von Wasser zur Abschreckung und durch die Eindüsung von ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltigen (NH4 +) Substanz werden aber reaktive Bestandteile des Gases, wie die Stickoxide (NOx), freies Chlor (Cl2) und gegebenenfalls radikalische Gasbestandteile wie nitrose Gase und radikalische Chlor-Sauerstoffverbindungen abgefangen, die ohne eine später folgende katalytische Umsetzung sonst zu einer vermehrten Bildung von Dioxinen und Furanen führen könnten. Auch können im Bypassabgas enthaltene Schwermetalle, Halogene und Schwefel und auch Kohlenmonoxid, das allerdings aufgrund der oxidativen Bedingungen im Drehrohrofen im Regelfall im Bypassabgas nicht zu erwarten ist, aber dennoch dort gelegentlich nachgewiesen wird, die später folgenden Katalysatoren vergiften. Die teilweise Umsetzung und Hydrolyse mit einer sehr komplexen Folgechemie kurzlebiger und reaktiver Verbindungen führt aber dazu, dass die klassischen Katalysatorgifte durch chemische Umsetzung maskiert werden.According to the invention, it is thus provided that the bypass exhaust gas withdrawn from the rotary kiln inlet chamber itself contains a high proportion of alkali metal (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth metal halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ) and sulfates (Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ) in the gas space, initially in to quench a device for cooling. The cooling of the bypass exhaust gases preferably takes place in a mixing chamber in which the hot bypass exhaust gases mix intimately with fresh atmospheric air or with water. The hot bypass exhaust gases are cooled to a temperature of 260 ° C to 400 ° C, preferably from 280 ° C to 380 ° C. During this strong cooling, the alkali (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ) resublimate and sulfate (Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ) and are present as dust in addition to raw meal in the bypass exhaust gas. The cooled, strongly dust-containing air is then mixed with an ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance in which, for example, gaseous ammonia gas (NH 3 ), an aqueous Urea solution (CH 4 N 2 O) or an aqueous ammonium solution (NH 4 + ) is supplied to between 260 ° C and 400 ° C, preferably 280 ° C and 380 ° C amount, cooled by-pass gas. At this temperature, which is clearly too low for the SNCR reaction, only partial to low conversion of nitrogen oxides (NO x ) takes place. By injecting water for quenching and by the injection of ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance but reactive components of the gas, such as the nitrogen oxides (NO x ), free chlorine (Cl 2 ) and optionally radical gas constituents such as nitrous gases and radical chlorine-oxygen compounds intercepted, which could otherwise lead to an increased formation of dioxins and furans without a subsequent catalytic reaction. Also contained in the bypass exhaust heavy metals, halogens and sulfur and carbon monoxide, which is, however, due to the oxidative conditions in the rotary kiln usually not expected in the bypass exhaust gas, but there is occasionally detected, poison the later following catalysts. The partial reaction and hydrolysis with a very complex subsequent chemistry of short-lived and reactive compounds, however, leads to the classical catalyst poisons being masked by chemical reaction.
Die Verweilzeit der ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltigen (NH4 +) Substanz in dem abgekühlten Bypassgas sollte so lange sein, dass ein erheblicher Anteil der radikalischen Gasbestandteile wie nitrose Gase und radikalische Chlor-Sauerstoffverbindungen umgesetzt werden. Der Eindüsung einer ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltigen (NH4 +) Substanz und die gemeinsame Verweilzeit in einer Leitung folgt die Einführung des Mischgases aus ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltigen (NH4 +) Substanz und dem abgekühlten, noch staubigen Bypassabgas in eine keramische Filteranordnung. Diese Filteranordnung wird deshalb aus Keramik gewählt, weil das ideale Temperaturfenster von 260°C bis 400°C, bevorzugt von 280°C bis 380°C für eine SCR-Reaktion (selective catalytic reduction) zu hoch ist für den Einsatz eines alternativen und kostengünstigeren Tuchfilters zur Entfernung des Staubes, nämlich Rohmehl und auskondensierte Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogenide (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfate (Li2SO4 , Na2SO4, K2SO4, MgSO4, CaSO4). Der im Vergleich zum Einsatz von Tuchfiltern sicherlich kostenintensivere Einsatz eines Keramikfilters lässt sich aber damit wirtschaftlich rechtfertigen, dass auf der Filteroberfläche des Keramikfilters Katalysatoren eingesetzt werden können, welche die Reaktion der ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltigen (NH4 +) Substanz mit den Stickoxiden (NOx) in den Bypassabgasen katalysieren. Die einsetzbaren Katalysatoren können unterschiedlicher Art sein. Die eine Art von Katalysatoren besteht im Wesentlichen aus Titandioxid (TiO2), Vanadiumpentoxid (V2O5) und Wolframdioxid (WO2) oder Mischkatalysatoren daraus. Die andere Art von Katalysatoren besteht aus Zeolithen. Katalysatoren aus (TiO2), Vanadiumpentoxid (V2O5) und Wolframdioxid (WO2) oder Mischkatalysatoren daraus oxidieren in Gegenwart von gasförmigen Halogenen (F2, Cl2, I2) auch das in Bypasabgasen möglicherweise vorhandene elementare Quecksilber (Hg), das sich dann besser in den Wäschern der Rauchgasentschwefelungsanlagen bzw. in den Filtern abscheiden lässt und nur noch zu einem geringeren Anteil (ca. 10%) an die Umgebung abgegeben wird. Ein weiterer Vorteil des Einsatzes von Titandioxid (TiO2), Vanadiumpentoxid (V2O5) und Wolframdioxid (WO2) oder Mischkatalysatoren daraus ist, dass diese Katalysatoren in Gegenwart von gasförmigen Halogenen (F2, Cl2, I2) die Bildung von Dioxinen (chlorierte und polychlorierte Dibenzodioxine) und Furanen (chlorierte und polychlorierte Dibenzofurane) unterdrücken. Um diese metallischen Katalysatoren nicht zu vergiften, ist die vorherige teilweise Umsetzung des Bypassabgases mit Wasser und ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltigen (NH4 +) Substanz vorteilhaft. Die Zeolith-basierten Katalysatoren sind in der Regel günstiger in der Anschaffung und sind weniger empfindlich gegenüber Abtragung und Vergiftung. Dafür aber haben sie den Nachteil, dass die Bildung von Dioxinen und Furanen nicht so gut unterdrückt wird. Zeolith-basierte Katalysatoren fördern den Zerfall von Dioxinen und Furanen im geringeren Ausmaße als die erwähnten metallischen Katalysatoren. Die wirtschaftlich günstigeren und robusteren, Zeolith-basierten Katalysatoren können daher eingesetzt werden, wenn die Trennung der Halogenide vom Bypassabgas vorher im keramischen Filter stattgefunden hat.The residence time of the ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance in the cooled bypass gas should be so long that a significant proportion of the radical gas constituents such as nitrous gases and free-radical Chlorine-oxygen compounds are reacted. The injection of an ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance and the common residence time in a line follows the introduction of the mixed gas of ammonia (NH 3 ), urea - (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance and the cooled, still dusty bypass exhaust gas in a ceramic filter assembly. This filter arrangement is selected from ceramic, because the ideal temperature window of 260 ° C to 400 ° C, preferably from 280 ° C to 380 ° C for a SCR reaction (Selective Catalytic Reduction) is too high for the use of an alternative and less expensive Cloth filter to remove the dust, namely raw meal and condensed alkali (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) and alkaline earth halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ) and sulfates (Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ). The use of a ceramic filter, which is certainly more cost-intensive than that of cloth filters, can be economically justified by using catalysts on the filter surface of the ceramic filter which allow the reaction of ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance with the nitrogen oxides (NO x ) catalyze in the bypass exhaust gases. The usable catalysts can be of different types. One type of catalyst consists essentially of titanium dioxide (TiO 2 ), vanadium pentoxide (V 2 O 5 ) and tungsten dioxide (WO 2 ) or mixed catalysts thereof. The other type of catalysts consists of zeolites. Catalysts of (TiO 2 ), vanadium pentoxide (V 2 O 5 ) and tungsten dioxide (WO 2 ) or mixed catalysts thereof in the presence of gaseous halogens (F 2 , Cl 2 , I 2 ) also oxidize the elemental mercury (Hg) possibly present in by-pass gases. , which can then be better separated in the scrubbers of the flue gas desulphurisation plants or in the filters and only to a lesser extent (about 10%) is released to the environment. Another advantage of the use of titanium dioxide (TiO 2 ), vanadium pentoxide (V 2 O 5 ) and tungsten dioxide (WO 2 ) or mixed catalysts thereof is that these catalysts in the presence of gaseous halogens (F 2 , Cl 2 , I 2 ) the formation of dioxins (chlorinated and polychlorinated dibenzodioxins) and furans (chlorinated and polychlorinated dibenzofurans). In order not to poison these metallic catalysts, the previous partial reaction of the bypass exhaust gas with water and ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance is advantageous. The zeolite-based catalysts are generally cheaper to buy and less sensitive to erosion and poisoning. But they have the disadvantage that the formation of dioxins and furans is not so well suppressed. Zeolite-based catalysts promote the decomposition of dioxins and furans to a lesser extent than the mentioned metallic catalysts. The more economically favorable and robust zeolite-based catalysts can therefore be used if the separation of the halides from the bypass exhaust gas has previously taken place in the ceramic filter.
In Ausgestaltung des erfindungsgemäßen Verfahrens ist vorgesehen, dass der Katalysator aus Titandioxid (TiO2), Vanadiumpentoxid (V2O5) und Wolframdioxid (WO2) besteht oder ein Mischkatalysatoren daraus ist, welcher Dioxine (chlorierte und polychlorierte Dibenzodioxine) und Furane (chlorierte und polychlorierte Dibenzofurane) abbaut.In an embodiment of the method according to the invention it is provided that the catalyst of titanium dioxide (TiO 2 ), vanadium pentoxide (V 2 O 5 ) and Tungsten dioxide (WO 2 ) or a mixed catalyst thereof, which degrades dioxins (chlorinated and polychlorinated dibenzodioxins) and furans (chlorinated and polychlorinated dibenzofurans).
In weiterer Ausgestaltung des erfindungsgemäßen Verfahrens ist vorgesehen, dass die Verweilzeit der abgekühlten Bypassabgase in einer Leitung zwischen der Vorrichtung zum Kühlen und der keramischen Filteranordnung so gewählt ist, dass die ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltige (NH4 +) Substanz die in dem abgekühlten Bypassgas befindlichen radikalischen Gasbestandteile wie nitrose Gase und radikalische Chlor-Sauerstoffverbindungen zu 50% durch Hydrolyse und/oder partieller Oxidation und/oder partieller Reduktion zu nicht radikalischen Gasbestandteilen umsetzt, bevorzugt mindestens zu 70%, besonders bevorzugt mindestens zu 95% umsetzt.In a further embodiment of the method according to the invention it is provided that the residence time of the cooled bypass exhaust gases in a line between the device for cooling and the ceramic filter assembly is selected so that the ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance in the cooled bypass gas located radical gas components such as nitrous gases and radical chlorine-oxygen compounds to 50% by hydrolysis and / or partial oxidation and / or partial reduction to non-radical gas components, preferably at least 70 %, particularly preferably at least 95%.
Korrespondierend zum erfindungsgemäßen Verfahren wird eine Anlage zur Herstellung von Zementklinker vorgeschlagen, wobei die Anlage in Gasflussrichtung einen Drehrohrofen zur Sinterung des Zementklinkers aufweist, und wobei der Drehrohrofen über eine Drehrohrofeneinlaufkammer mit einem Calcinator zur Entsäuerung von Rohmehl oder mit einem Drehrohrofensteigeschacht verbunden ist, und in welcher ein Bypassabgas im Bereich der Drehrohrofeneinlaufkammer abgezogen wird, gekennzeichnet durch dass eine Vorrichtung zum Abkühlen des Bypassabgases vorgesehen ist, welche das Bypassabgas auf eine Temperatur zwischen 260°C und 400°C, bevorzugt zwischen 280°C und 380°C in abkühlt, vorzugsweise eine Mischkammer, welche das Bypassabgas mit Luft und/oder Wasser vermischt, dass darauf folgend eine Vorrichtung zum Eindüsen einer ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltigen (NH4 +) Substanz in das gekühlte Bypassabgas vorgesehen ist, wobei der Ammoniak (NH3), der Harnstoff (CH4N2O) oder das Ammonium (NH4 +) die in dem abgekühlten Bypassabgas befindlichen radikalischen Gasbestandteile wie nitrose Gase und radikalische Chlor-Sauerstoffverbindungen durch Hydrolyse und/oder partieller Oxidation und/oder partieller Reduktion zumindest teilweise zu nicht radikalischen Gasbestandteilen umsetzt, dass darauffolgend eine keramische Filteranordnung vorgesehen ist, welche das beim vorherigen Abkühlen des Bypassabgases ausgefallene Lithiumfluorid (LiF), Lithiumchlorid (LiCl), Natriumfluorid (NaF), Natriumchlorid (NaCl), Kaliumchlorid (KCl), Lithiumsulfat (Li2SO4), Natriumsulfat (Na2SO4), Kaliumsulfat (K2SO4) und gegebenenfalls weitere Halogenide (I-) und Sulfate (SO4 –) der Alkali- (Li, Na, K) und Erdalkalimetalle (Mg, Ca) ausfiltert, und das durch die ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltige (NH4 +) Substanz noch nicht reduzierte Stickoxid (NOx) an einem in der keramischen Filteranordnung vorhandenen und/oder der keramischen Filteranordnung unmittelbar folgenden vorhandenen Katalysator chemisch selektiv reduziert (SCR, selective catalytic reduction), wobei der Katalysator auf Filterelementen der keramischen Filteranordnung, auf einem separatem Träger in der keramischen Filteranordnung integriert, und/oder der keramischen Filteranordnung unmittelbar folgend in einem eigenen Reaktor angeordnet ist.Corresponding to the method according to the invention a plant for the production of cement clinker is proposed, wherein the plant in the gas flow direction has a rotary kiln for sintering the cement clinker, and wherein the rotary kiln is connected via a Drehrohrofeneinlaufkammer with a calciner for deacidification of raw meal or with a rotary kiln riser shaft, and in which a bypass exhaust gas is withdrawn in the region of the rotary kiln inlet chamber, characterized in that a device for cooling the bypass exhaust gas is provided, which cools the bypass exhaust gas to a temperature between 260 ° C and 400 ° C, preferably between 280 ° C and 380 ° C, preferably a Mixing chamber, which mixes the bypass exhaust gas with air and / or water, followed by a device for injecting an ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance in the cooled Bypass exhaust gas is provided, wherein the ammonia (NH 3 ), the Ha (CH 4 N 2 O) or the ammonium (NH 4 + ) located in the cooled bypass exhaust gas radical components such as nitrous gases and radical chlorine-oxygen compounds by hydrolysis and / or partial oxidation and / or partial reduction at least partially to non-radical gas components implements that a ceramic filter arrangement is then provided which measures the lithium fluoride (LiF), lithium chloride (LiCl), sodium fluoride (NaF), sodium chloride (NaCl), potassium chloride (KCl), lithium sulfate (Li 2 SO 4 ) precipitated during the previous cooling of the bypass exhaust gas. , Sodium sulfate (Na 2 SO 4 ), potassium sulfate (K 2 SO 4 ) and optionally further halides (I) and sulfates (SO 4 - ) of the alkali (Li, Na, K) and alkaline earth metals (Mg, Ca) filtered out, and by the ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance not yet reduced nitrogen oxide (NO x ) on a present in the ceramic filter assembly and or the ceramic filter assembly immediately following existing catalyst chemically selectively reduced (SCR, selective catalytic reduction), wherein the catalyst on filter elements of the ceramic filter assembly, integrated on a separate support in the ceramic filter assembly, and / or the ceramic filter assembly immediately following in its own Reactor is arranged.
In Ausgestaltung der erfindungsgemäßen Anlage ist vorgesehen, dass der Katalysator aus Titandioxid (TiO2), Vanadiumpentoxid (V2O5) und Wolframdioxid (WO2) besteht oder ein Mischkatalysator daraus ist, welcher Dioxine (chlorierte und polychlorierte Dibenzodioxine) und Furane (chlorierte und polychlorierte Dibenzofurane) abbaut.In an embodiment of the system according to the invention it is provided that the catalyst consists of titanium dioxide (TiO 2 ), vanadium pentoxide (V 2 O 5 ) and tungsten dioxide (WO 2 ) or a mixed catalyst thereof, which dioxins (chlorinated and polychlorinated dibenzodioxins) and furans (chlorinated and polychlorinated dibenzofurans) degrades.
In weiterer Ausgestaltung der erfindungsgemäßen Anlage ist vorgesehen, durch Auslegung einer Leitung die Verweilzeit der abgekühlten Bypassabgase in der Leitung zwischen der Vorrichtung zum Kühlen und der keramischen Filteranordnung so gewählt ist, dass die ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltige (NH4 +) Substanz die in dem abgekühlten Bypassgas befindlichen radikalischen Gasbestandteile wie nitrose Gase und radikalische Chlor-Sauerstoffverbindungen zu 50% durch Hydrolyse und/oder partieller Oxidation und/oder partieller Reduktion zu nicht radikalischen Gasbestandteilen umsetzt, bevorzugt mindestens zu 70%, besonders bevorzugt mindestens zu 95% umsetzt.In a further embodiment of the system according to the invention is provided by designing a line, the residence time of the cooled bypass exhaust gases in the line between the device for cooling and the ceramic filter assembly is selected so that the ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance in the cooled bypass gas located radical gas components such as nitrous gases and radical chlorine-oxygen compounds to 50% by hydrolysis and / or partial oxidation and / or partial reduction to non-radical gas components, preferably at least 70%, more preferably at least 95%.
Die Erfindung wird anhand der folgenden Figuren näher erläutert. Es zeigt:The invention will be explained in more detail with reference to the following figures. It shows:
In
Eine zur Anlagenkonfiguration in
In
Die Erfindung macht sich im Wesentlichen den Gedanken zu nutze, das Bypassabgas erst abzukühlen, um die beim Abkühlen kondensierenden und erstarrenden oder resublimierenden Alkali- (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) und Erdalkalihalogenide (MgF2, MgCl2, MgI2, CaF2, CaCl2, CaI2) und -sulfate (Li2SO4 , Na2SO4, K2SO4, MgSO4, CaSO4) abzuscheiden. Erst danach findet eine katalytische Umsetzung der unerwünschten Stickoxide über ein SCR-Verfahren statt. Da das SCR-Verfahren nicht einsetzbar wäre, wenn gattungsgemäße Tuchfilter eingesetzt würden, weil die Tuchfilter der Temperatur nicht standhalten würden, wird erfindungsgemäß ein keramischer Filter eingesetzt. Der wirtschaftliche Nachteil des keramischen Filters gegenüber einem Tuchfilter wird aber dadurch ausgeglichen, dass der keramischen Filter gleichzeitig als Träger für den Katalysator dienen kann. Um die Schadstoffe möglichst quantitativ abzuscheiden, verweilt das Reduktionsmittel, die ammoniak- (NH3), harnstoff- (CH4N2O) und/oder ammoniumhaltigen (NH4 +) Substanz, mit dem abgekühlten Bypassabgas vor der Entstaubung und Abscheidung der Halogenide und Sulfate. The invention essentially makes use of the idea of first cooling the bypass exhaust gas in order to cool the alkali (LiF, LiCl, LiI, NaF, NaCl, NaI, KF, KCl, KI) condensing and resolidifying on cooling and alkaline earth metal halides (MgF 2 , MgCl 2 , MgI 2 , CaF 2 , CaCl 2 , CaI 2 ) and sulfates (Li 2 SO 4 , Na 2 SO 4 , K 2 SO 4 , MgSO 4 , CaSO 4 ). Only then does a catalytic conversion of the unwanted nitrogen oxides take place via an SCR process. Since the SCR method would not be usable if generic cloth filters would be used because the cloth filters would not withstand the temperature, a ceramic filter is used according to the invention. However, the economic disadvantage of the ceramic filter over a cloth filter is compensated by the fact that the ceramic filter can simultaneously serve as a carrier for the catalyst. To remove the pollutants as quantitatively as possible, dwells the reducing agent, the ammonia (NH 3 ), urea (CH 4 N 2 O) and / or ammonium-containing (NH 4 + ) substance, with the cooled bypass exhaust gas before the dedusting and deposition of the halides and sulfates.
BezugszeichenlisteLIST OF REFERENCE NUMBERS
- 100100
- Anlagenkonfigurationsystem configuration
- 101101
- Verbrennungsgasecombustion gases
- 102102
- DrehrohrofenRotary kiln
- 103103
- Zementklinkercement clinker
- 104104
- DrehrohrofeneinlaufkammerRotary kiln inlet chamber
- 105105
- Gasstromgas flow
- 106106
- Gasstromgas flow
- 107107
- Calcinatorcalciner
- 108108
- Gasstromgas flow
- 109109
- Mischkammermixing chamber
- 110110
- atmosphärische Luft/Wasseratmospheric air / water
- 111111
- Verdichtercompressor
- 112112
- Mischgasemixed gases
- 113113
- Leitungmanagement
- 114114
- FilteranordnungA filter assembly
- 115115
- Zellradschleuserotary valve
- 116116
- Katalysatorcatalyst
- 117117
- Filterelementefilter elements
- 118118
- Leitungmanagement
- 119119
- Verdichtercompressor
- 120120
- Kaminfireplace
- 200200
- Anlagenkonfigurationsystem configuration
- 201201
- Verbrennungsgasecombustion gases
- 202202
- DrehrohrofenRotary kiln
- 203203
- Zementklinkercement clinker
- 204204
- DrehrohrofeneinlaufkammerRotary kiln inlet chamber
- 205205
- Gasstromgas flow
- 206206
- Gasstromgas flow
- 207207
- Calcinatorcalciner
- 208208
- Gasstromgas flow
- 209209
- Mischkammermixing chamber
- 210210
- atmosphärische Luft/Wasseratmospheric air / water
- 211211
- Verdichtercompressor
- 212212
- Mischgasemixed gases
- 213213
- Leitungmanagement
- 214214
- FilteranordnungA filter assembly
- 215215
- Zellradschleuserotary valve
- 216216
- Katalysatorcatalyst
- 216'216 '
- Trägercarrier
- 217217
- Filterelementefilter elements
- 118118
- Leitungmanagement
- 119119
- Verdichtercompressor
- 220220
- Kaminfireplace
- 300300
- Anlagenkonfigurationsystem configuration
- 301301
- Verbrennungsgasecombustion gases
- 302302
- DrehrohrofenRotary kiln
- 303303
- Zementklinkercement clinker
- 304304
- DrehrohrofeneinlaufkammerRotary kiln inlet chamber
- 305305
- Gasstromgas flow
- 306306
- Gasstromgas flow
- 307307
- Calcinatorcalciner
- 308308
- Gasstromgas flow
- 309309
- Mischkammermixing chamber
- 310310
- atmosphärische Luft/Wasseratmospheric air / water
- 311311
- Verdichtercompressor
- 312312
- Mischgasemixed gases
- 313313
- Leitungmanagement
- 314314
- FilteranordnungA filter assembly
- 315315
- Zellradschleuserotary valve
- 316316
- Katalysatorcatalyst
- 316'316 '
- Reaktorreactor
- 317317
- Filterelementefilter elements
- 318318
- Leitungmanagement
- 319319
- Verdichtercompressor
- 320320
- Kaminfireplace
ZITATE ENTHALTEN IN DER BESCHREIBUNG QUOTES INCLUDE IN THE DESCRIPTION
Diese Liste der vom Anmelder aufgeführten Dokumente wurde automatisiert erzeugt und ist ausschließlich zur besseren Information des Lesers aufgenommen. Die Liste ist nicht Bestandteil der deutschen Patent- bzw. Gebrauchsmusteranmeldung. Das DPMA übernimmt keinerlei Haftung für etwaige Fehler oder Auslassungen.This list of the documents listed by the applicant has been generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.
Zitierte PatentliteraturCited patent literature
- DE 19718259 A2 [0004] DE 19718259 A2 [0004]
- DE 10158968 A2 [0008] DE 10158968 A2 [0008]
Claims (6)
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102013016701.9A DE102013016701B4 (en) | 2013-10-08 | 2013-10-08 | Process for the denitrification of bypass exhaust gases in a plant for the production of cement clinker and plant for the production of cement clinker |
DK14789191T DK3055266T3 (en) | 2013-10-08 | 2014-10-06 | Process for cleaning bypass gases in a cement clinker plant |
RU2016115625A RU2668445C2 (en) | 2013-10-08 | 2014-10-06 | Method for denitrification of bypass exhaust gases in plant for producing cement clinker |
US15/027,626 US9914664B2 (en) | 2013-10-08 | 2014-10-06 | Method for denitrification of bypass exhaust gases in a plant for producing cement clinker |
EP14789191.5A EP3055266B1 (en) | 2013-10-08 | 2014-10-06 | Method for the denitrification of bypass exhaust gases in a plant for producing cement clinker |
CN201480064045.3A CN105829261B (en) | 2013-10-08 | 2014-10-06 | The method of bypass exhaust denitrogenation is given in the device of production cement clinker |
PCT/EP2014/071317 WO2015052123A1 (en) | 2013-10-08 | 2014-10-06 | Method for the denitrification of bypass exhaust gases in a plant for producing cement clinker |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102013016701.9A DE102013016701B4 (en) | 2013-10-08 | 2013-10-08 | Process for the denitrification of bypass exhaust gases in a plant for the production of cement clinker and plant for the production of cement clinker |
Publications (2)
Publication Number | Publication Date |
---|---|
DE102013016701A1 true DE102013016701A1 (en) | 2015-04-09 |
DE102013016701B4 DE102013016701B4 (en) | 2017-06-14 |
Family
ID=51794848
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DE102013016701.9A Withdrawn - After Issue DE102013016701B4 (en) | 2013-10-08 | 2013-10-08 | Process for the denitrification of bypass exhaust gases in a plant for the production of cement clinker and plant for the production of cement clinker |
Country Status (7)
Country | Link |
---|---|
US (1) | US9914664B2 (en) |
EP (1) | EP3055266B1 (en) |
CN (1) | CN105829261B (en) |
DE (1) | DE102013016701B4 (en) |
DK (1) | DK3055266T3 (en) |
RU (1) | RU2668445C2 (en) |
WO (1) | WO2015052123A1 (en) |
Cited By (11)
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DE102015002688B3 (en) * | 2015-03-04 | 2016-05-19 | Khd Humboldt Wedag Gmbh | Process and plant for the denitrification of bypass exhaust gases in a multi-stage system of mixing chambers in a plant for the production of cement clinker |
EP3115345A1 (en) * | 2015-07-09 | 2017-01-11 | Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH | Method and apparatus for producing cement clinker |
DE102015111974A1 (en) * | 2015-07-23 | 2017-01-26 | Thyssenkrupp Ag | Process and plant for the production of cement clinker or other mineral products and for denitrification of bypass gases |
AT517813A1 (en) * | 2015-09-08 | 2017-04-15 | Holcim Technology Ltd | Method and apparatus for reducing the NOx emissions of a rotary kiln |
WO2018073239A1 (en) * | 2016-10-17 | 2018-04-26 | Thyssenkrupp Industrial Solutions Ag | Method and installation for cleaning pre-heater exhaust gases of an installation for the cement and/or mineral industry |
IT201700059650A1 (en) * | 2017-05-31 | 2018-12-01 | Cimprogetti S R L | REGENERATIVE LIME-OVEN WITH A PARALLEL FLOW WITH A SYSTEM FOR FILLING NITROGEN OXIDES AND THEIR MIXES IN EXIT SMOKES |
EP3294441A4 (en) * | 2015-05-12 | 2018-12-05 | FLSmidth A/S | Nox reduction process in a cement kiln manufacturing system |
EP3219689B1 (en) | 2016-03-18 | 2018-12-12 | Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH | Cement clinker line and a method for operating a cement clinker line |
DE102020202322A1 (en) | 2020-02-24 | 2021-08-26 | Ibu-Tec Advanced Materials Ag | Device for the thermal treatment of a raw material |
CN113790589A (en) * | 2021-09-22 | 2021-12-14 | 新疆宜化化工有限公司 | Process and device for realizing energy-saving and efficient drying of carbide slag |
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CN107321183B (en) * | 2017-08-30 | 2020-09-01 | 中国启源工程设计研究院有限公司 | SCR denitrification facility |
CN108298844A (en) * | 2018-04-08 | 2018-07-20 | 天津健威泽节能环保科技股份有限公司 | A kind of clinker drop alkali device and implementation method |
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WO2022053986A1 (en) * | 2020-09-09 | 2022-03-17 | Flsmidth A/S | Cement kiln bypass emissions reduction |
CN114028942B (en) * | 2021-12-01 | 2024-07-09 | 沈阳铝镁设计研究院有限公司 | Device and method for preventing SCR reactor from being blocked and catalyst from being poisoned |
DE102022201570A1 (en) * | 2022-02-16 | 2023-08-17 | Sms Group Gmbh | Method and device for treating primary gas from a metallurgical vessel |
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- 2014-10-06 RU RU2016115625A patent/RU2668445C2/en active
- 2014-10-06 CN CN201480064045.3A patent/CN105829261B/en active Active
- 2014-10-06 WO PCT/EP2014/071317 patent/WO2015052123A1/en active Application Filing
- 2014-10-06 DK DK14789191T patent/DK3055266T3/en active
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DE19718259A1 (en) | 1997-04-30 | 1998-11-05 | Kloeckner Humboldt Wedag | Process and plant for reducing pollutant cycles in the production of cement clinker from raw meal |
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Cited By (15)
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DE102015002688B3 (en) * | 2015-03-04 | 2016-05-19 | Khd Humboldt Wedag Gmbh | Process and plant for the denitrification of bypass exhaust gases in a multi-stage system of mixing chambers in a plant for the production of cement clinker |
EP3294441A4 (en) * | 2015-05-12 | 2018-12-05 | FLSmidth A/S | Nox reduction process in a cement kiln manufacturing system |
EP3115345A1 (en) * | 2015-07-09 | 2017-01-11 | Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH | Method and apparatus for producing cement clinker |
WO2017005724A1 (en) * | 2015-07-09 | 2017-01-12 | Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH | Method and apparatus for producing cement clinker |
US10457599B2 (en) | 2015-07-09 | 2019-10-29 | Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH | Method and apparatus for producing cement clinker |
DE102015111974A1 (en) * | 2015-07-23 | 2017-01-26 | Thyssenkrupp Ag | Process and plant for the production of cement clinker or other mineral products and for denitrification of bypass gases |
AT517813A1 (en) * | 2015-09-08 | 2017-04-15 | Holcim Technology Ltd | Method and apparatus for reducing the NOx emissions of a rotary kiln |
EP3219689B1 (en) | 2016-03-18 | 2018-12-12 | Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH | Cement clinker line and a method for operating a cement clinker line |
EP3219689B2 (en) † | 2016-03-18 | 2022-04-06 | Südbayerisches Portland-Zementwerk Gebr. Wiesböck & Co. GmbH | Cement clinker line and a method for operating a cement clinker line |
WO2018073239A1 (en) * | 2016-10-17 | 2018-04-26 | Thyssenkrupp Industrial Solutions Ag | Method and installation for cleaning pre-heater exhaust gases of an installation for the cement and/or mineral industry |
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IT201700059650A1 (en) * | 2017-05-31 | 2018-12-01 | Cimprogetti S R L | REGENERATIVE LIME-OVEN WITH A PARALLEL FLOW WITH A SYSTEM FOR FILLING NITROGEN OXIDES AND THEIR MIXES IN EXIT SMOKES |
DE102020202322A1 (en) | 2020-02-24 | 2021-08-26 | Ibu-Tec Advanced Materials Ag | Device for the thermal treatment of a raw material |
CN113790589A (en) * | 2021-09-22 | 2021-12-14 | 新疆宜化化工有限公司 | Process and device for realizing energy-saving and efficient drying of carbide slag |
WO2024026522A1 (en) * | 2022-08-03 | 2024-02-08 | Scheuch Management Holding GmbH | Method for producing cement with sluice devices, filter system and cement production system |
Also Published As
Publication number | Publication date |
---|---|
EP3055266B1 (en) | 2019-08-21 |
DK3055266T3 (en) | 2019-11-25 |
RU2016115625A (en) | 2017-11-14 |
WO2015052123A1 (en) | 2015-04-16 |
US20160347657A1 (en) | 2016-12-01 |
US9914664B2 (en) | 2018-03-13 |
EP3055266A1 (en) | 2016-08-17 |
CN105829261A (en) | 2016-08-03 |
DE102013016701B4 (en) | 2017-06-14 |
CN105829261B (en) | 2018-11-16 |
RU2668445C2 (en) | 2018-10-01 |
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